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US20040156765A1 - Gold and silver recovery from polymetallic sulfides by treatment with halogens - Google Patents

Gold and silver recovery from polymetallic sulfides by treatment with halogens Download PDF

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Publication number
US20040156765A1
US20040156765A1 US10/706,325 US70632503A US2004156765A1 US 20040156765 A1 US20040156765 A1 US 20040156765A1 US 70632503 A US70632503 A US 70632503A US 2004156765 A1 US2004156765 A1 US 2004156765A1
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solution
gold
silver
produce
granules
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Jean-Marc Lalancette
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Nichromet Extraction Inc
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Nichromet Extraction Inc
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Priority to US10/706,325 priority Critical patent/US20040156765A1/en
Assigned to NICHROMET EXTRACTION INC. reassignment NICHROMET EXTRACTION INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: LALANCETTE, JEAN-MARC
Publication of US20040156765A1 publication Critical patent/US20040156765A1/en
Priority to US11/937,815 priority patent/US7537741B2/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to gold and silver recovery from polymetallic sulfides by treatment with halogens.
  • gold recovery can be as high as 98%. This process calls for a contact time of one to three days at near ambient temperature in the presence of air.
  • the cyanide process performs very poorly. Ores refractory to cyanide extraction can be grouped under the general term of polymetallic ores. In such ores, one finds small amounts of base metals such as copper or zinc, typically 0.1% Cu or 0.3% Zn. Such small amounts qualify the ore as of very low grade for the production of copper or zinc. If such a polymetallic ore body contains some gold (for example, 4 g/T Au or Ag or a mixture of both), the cyanide extraction process does not perform well. The poor performance is due to the base metals, either copper or zinc, (as well as silver), having a much stronger ability to form complexes with cyanide than gold.
  • Polymetallic ores constitute complex mixtures of sulfides.
  • This sulfur is prone to bio-oxidation ( Thiobacillus ferrooxidans ), and the resulting drainage is quite acidic and toxic due to its metallic content.
  • the present invention seeks to meet these and other needs.
  • the present invention relates to a method for treating a polymetallic sulfide ore containing gold and/or silver, and further containing base metals selected from the group consisting of iron, aluminum, chromium, titanium, copper, zinc, lead, nickel, cobalt, mercury, tin, and mixtures thereof, comprising the steps of:
  • the present invention further relates to a method for the recovery of gold and silver from polymetallic sulfide ores, characterized by low operational and cost investments.
  • the present invention also relates to a method for the recovery of gold and silver from polymetallic sulfide ores, characterized by being carried out at atmospheric pressure and at low oxidation temperatures prior to leaching.
  • the present invention relates to a method for the recovery of gold and silver from polymetallic sulfide ores, characterized by producing tailings devoid of elemental sulfur, sulfides, or soluble sulfates and by fast reaction rates allowing for high rates of treatment.
  • the present invention relates to a method for the recovery of precious metals such as gold and silver, as well as base metals such as copper, nickel, cobalt, zinc, tin and lead from polymetallic sulfide ores, in addition to relating to the safe removal of sulfur, arsenic and mercury as well as to the disposal of iron, chromium, aluminum and titanium in an inert and insoluble form.
  • FIG. 1 is a block diagram illustrating the various steps of the method of the present invention
  • FIG. 2 is a block diagram illustrating the various steps of the sulfur removal aspect of the method of the present invention.
  • FIG. 3 is a block diagram illustrating the various steps of the gold and silver recovery aspect of the method of the present invention.
  • FIG. 4 is a block diagram illustrating the various steps of the base metal recovery aspect of the method of the present invention.
  • FIG. 5 is a schematic illustration of an electrolytic cell used in the method of the present invention.
  • the present invention relates to a new method for the recovery of precious metals such as gold and silver from polymetallic sulfide ores.
  • the present invention also relates to the safe removal of sulfur, arsenic and mercury as well as to the disposal of iron, chromium, aluminum and titanium in an inert and insoluble form. This is achieved at considerably lower cost than with the current chloridation or cyanide processes, by avoiding sulfur oxidation by electrochemical means.
  • the method of the present invention is very time efficient, of the order of a few hours, and is carried out at atmospheric pressure and at oxidation temperatures of at least about 300° C. and preferably ranging from about 400 to about 600° C. The method allows for the separation of the precious metals as well as the base metals from the common metals, while recycling the reagents and releasing only inert waste materials into the environment.
  • gold and silver, and optionally base metals such as copper, zinc, lead, tin, nickel, cobalt and mercury can be recovered from polymetallic sulfide ores in yields generally well above 80% by the method of the present invention comprising the following preferred steps:
  • oxidizing the polymetallic sulfide ore preferably using lean air having about 10% O 2 , at a temperature ranging from about 400 to about 600° C., to reduce the sulfur content of the ore to about 0.5% S (as sulfide) or less. Temperatures above 600° C. are also suitable but energy consumption is increased and sintering of the ore results.
  • the resulting SO 2 is fixed by calcium carbonate as calcium sulfite, which auto-oxidizes to calcium sulfate dihydrate (gypsum). This results in the elimination of sulfur in a manner compatible with environmental regulations;
  • the chlorine/HCl/hypochlorous acid solution containing a catalytic amount of bromine, is generated by circulating a portion of the brine solution used to slurry the oxidized ore through the anodic compartment of an electrolytic cell, at a rate sufficient to dissolve the chlorine in the brine solution.
  • the ore is maintained in suspension in the acidic halogenated brine at a temperature ranging from about 35-45° C. by slow stirring, without aeration, for a period of 2-3 hours for most ores, and up to 5 hours for exceptionally refractory ores.
  • the combined filtrate and rinsings are circulated over activated carbon for gold and silver recovery; and
  • Raising the pH to about 2.5-3.5 induces the precipitation of iron, aluminum, chromium and titanium as insoluble oxides of these metals, in various hydrated forms. These oxides are filtered and washed with brine. Raising the pH of the resulting filtrate to values above 3.5, induces the precipitation of the base metals such as copper, zinc, lead, tin, nickel and cobalt as a base metal concentrate.
  • the brine solution following the removal of the metals, is recirculated for further leaching.
  • the sterile solids are rinsed with water and the rinsings concentrated by evaporation, using waste heat from the sulfide oxidation step.
  • the concentrated rinsings, along with the brine solution, are then recycled so as to prevent salt losses or salt release into the environment.
  • the gold and/or silver containing ore additionally comprising variable amounts of base metals such as Cu, Zn, Pb, Sn, Ni, and Co, is a sulfide or complex sulfide.
  • the ore may further incorporate one or more other common metals such as iron, aluminum, titanium, chromium, as well as elements such as arsenic, antimony or bismuth. Mercury is occasionally also present in the ore.
  • the ore is reduced to a particle size of less than about 140 mesh by standard methods known in the art, such as crushing.
  • the sulfur content of the ore which can be as high as 15%, is reduced to about 0.5% or less (as sulfides) by controlled oxidation in a reactor or kiln.
  • the reactor or kiln provides for a control of the oxygen content in the reaction chamber.
  • a relatively low oxidation temperature typically ranging from about 400 to about 600° C., is very advantageous since it prevents any sintering of the material and generates a solid product having a large surface area and having good reactivity.
  • This treatment is much preferred to standard roasting where temperatures as high as 1200° C. have been observed. Such high reaction temperatures induce much sintering and volatilization.
  • Standard roasting involves the free burning of the sulfides in the presence of excess air.
  • the control of the low oxidation temperatures is achieved by recycling part of the lean air back to the reactor. This allows for the oxygen content in the reactor to be maintained at values not exceeding 10% O 2 . It is important to prevent sodium chloride present in the ore from being oxidized. It is well known that sodium chloride contaminations as low as 0.01 percent, can induce significant volatilization of gold and silver.
  • the gas stream from the oxidation reactor is cooled in a settling chamber, allowing for the collection of volatile oxides such as arsenic oxide, traces of zinc oxide, and metallic mercury if present in the starting ore, as well as other products generated during the oxidative treatment. Dusts carried mechanically from the fines in the reactor are also collected in the settling chamber. The amount of solids collected is generally small; less than one percent of the weight of the ore treated. The solids thus collected can be recovered and used for recuperation of values such as As 2 O 3 or mercury, or they can be safely disposed of in sealed containers.
  • the gas at the exit of the settling chamber essentially composed of SO 2 and lean air, is partly redirected back to the oxidation reactor for oxygen level control, and partly directed to a SO 2 scrubbing unit.
  • the SO 2 is adsorbed using a finely divided limestone slurry (200 mesh), allowing for the transformation of essentially all of the SO 2 (about 98%) into calcium sulfite, which auto-oxidizes to calcium sulfate dihydrate or gypsum.
  • Gypsum is a very stable and inert product representing a definitive solution for the safe disposal of sulfur. It can be used as a building material in the production of Portland cement or as land fill.
  • the water following the dewatering of the gypsum is recirculated back to a water thank. Since gypsum is a dihydrate, there is a net consumption of water in the scrubbing process.
  • the gases freed of SO 2 are vented through a flue duct.
  • the ore was made more reactive towards leaching, and essentially all of the sulfur initially present has been disposed of in a safe and environmentally compatible manner.
  • the present approach constitutes an economically attractive alternative to the presently available methods.
  • the current cost of electrochemically oxidizing 1% of sulfur in one metric ton of sulfide ore is $US 4.71 per unit percent of S 2 ⁇ per ton with a KWh at $US 0.09 per kilowatt and with an efficiency of 80%.
  • the cost of oxidizing the sulfide content of an ore containing 10% S 2 ⁇ to elemental sulfur, using an electrochemically-produced reagent such as chlorine, would be in the best case scenario $US 47.10 per ton of ore for power only.
  • the controlled oxidation of the sulfur content using lean air can be done at 10% or less of that cost, and transforms the sulfur into a safe and environmentally disposable form.
  • the electrochemical oxidation process leaves elemental sulfur in the tailings generating a potential source of acid drainage.
  • the leaching solution is a brine solution having a high concentration of chloride, i.e. from 275 to 300 g/l of NaCl or from 190 to 225 g/l of KCl. Lower salt concentrations yielded lower percentages of silver recovery, when silver was associated with gold in the oxidized ore.
  • the bromide ion will be reduced first, followed by some chloride ions so as to give a mixture of halogens dissolved in the brine solution.
  • the brine solution containing dissolved Cl 2 and Br 2 is mixed with fresh brine from a brine tank to provide a volume of liquid necessary to form a 20% slurry with the oxidized ore in a reactor kept at 35-45° C. The slurry is slowly stirred in order to prevent settling of the ore.
  • hypochlorous acid could account for the observed chloridation of gold by chlorine in the presence of water.
  • a similar equation can be written to describe the behavior of bromine, which is in equilibrium with hydrobromic acid and hypobromous acid.
  • the solubilized species can therefore be seen as a mixture of chlorides and hypochlorides, which eventually end up as chlorides when the hypochlorous ion decomposes with the concomitant evolution of nascent oxygen (Eq. IX):
  • the duration of the leaching usually ranges from 2 to 3 hours. With exceedingly refractory ores it is necessary to extend the contact time to, for example, about 5 hours.
  • the slurry is filtered or centrifuged, producing a pregnant solution and a waste or barren solid.
  • the barren solid was first rinsed with brine in order to recover any held-up values in the cake, followed by washing with water to recover any salt.
  • the so-obtained tailings contain arsenic as an iron arsenate, and are free of sulfur and of soluble base metals.
  • the pregnant solution is circulated over carbon to collect the gold and silver. Following the recovery of gold and silver from the carbon by known methods, these precious metals are obtained by electrowinning or other standard techniques such as ion exchange and precipitation. The gold/silver-free solution is then recovered to be further treated so as to collect the base metals.
  • the base metals to be obtained from the leaching of gold-bearing polymetallic sulfide ores are of two categories.
  • the first category contains metals of relatively high commercial value, often obtained by pyrometallurgical operations. This category contains metals such as nickel, cobalt, copper, zinc, lead, tin and mercury.
  • the second category contains metals of low economic value, and comprises predominantly iron with considerably smaller amounts of aluminum, titanium, chromium and traces of the p-bloc elements.
  • sodium hydroxide is generated in the cathodic compartment of the electrolytic cell.
  • the sodium hydroxide solution is accumulated in a caustic tank and is then used to raise the pH of the previously produced barren solution, devoid of gold and silver, leaving the carbon columns, from below 1 to about 2.5 to about 3.5.
  • any iron existing as Fe +3 is instantaneously precipitated by hydrolysis as a hydrated iron oxide. Titanium, aluminum and chromium react similarly within this pH range. The hydrated oxides are removed by filtration.
  • the solids are rinsed with brine in order to recuperate any base metals of values held up in the solid cake, followed by washing with water to remove any traces of salt.
  • the salt-free mixture of oxides is then discarded as an insoluble and inert material of little or no commercial value.
  • the solution obtained from the filtration and the brine rinsings contains the base metals of value.
  • Mercury if present, was recovered on carbon together with gold and silver.
  • the pH of the mercury-free solution pH between about 2.5-3.5, is further raised using an additional portion of the sodium hydroxide solution to values above 3.5, causing all of the base metals (Ni, Co, Cu, Zn, Pb, Sn) to precipitate as oxides or hydrated oxides.
  • the oxides are removed from the mixture by filtration and are rinsed with water to remove any traces of salt, to provide a concentrate of metals having significant commercial value.
  • the brine being free of metals, is recycled back to the fresh brine reservoir.
  • the rinsings are concentrated by evaporation so as to give a brine solution of appropriate concentration, and which is also recycled back to the fresh brine reservoir.
  • a Canadian ore sample (90 g) from the Sudbury (Ontario) area containing 4.5 g/T Au, 8 g/T Ag, 0.1% As, 7.5% S, 5.5% Fe, 0.1% Ni, 0.008 Co and 0.5% Cu was reduced to a particle size of about 140 mesh and heated at 585-600° C. in an atmosphere composed of N 2 (50%) and air (50%), over a period of two hours in a VycorTM tube heated externally in a LindbergTM furnace. The temperature was measured inside the mass being oxidized. The external heating was reduced when the oxidation began at around 400° C.
  • a sample of the oxidized material (25.0 g) was placed in a three-necked one liter flask, along with 500 g of water, 150 g of sodium chloride and 1.2 g of sodium bromide. The suspension was stirred magnetically and the flask was closed so as to exclude air from entering the system.
  • the slurry was extracted from the flask through one of the necks using a peristaltic pump, and was subsequently circulated through the anodic compartment of an electrolytic cell operating with a brine solution having the same concentration as the brine solution in the flask (anode of graphite, operation at 2.5 V).
  • the anodic fluid was returned to the flask after dissolving chlorine.
  • the cell was operated on and off in such a manner as to maintain a slight reddish coloration in the flask indicative of the presence of free bromine.
  • the reaction flask was maintained at 40° C. for a period of 2.5 hours after which it was filtered on a Buchner funnel.
  • the solid was rinsed three times with a brine solution containing 300 g/l NaCl.
  • the mixed filtrate and rinsings were very acid, having a pH below 1.0.
  • the acidic filtrate and rinsings were then treated with 30 g of carbon (NoritTM RO3515) so as to collect gold and silver.
  • the barren solid was then rinsed with water to completely remove any traces of brine (negative test to AgNO 3 ), dried at 110° C. (16.8 g) and submitted to elemental analysis.
  • the elemental analysis indicated that 96% of the gold and 94% of the silver initially present in the oxidized material, were leached out and then adsorbed on the carbon.
  • KCl brine 50.0 g of oxidized ore in 500 mL of KCl brine (200 g KCl/L) containing 2.0 g KBr.
  • the suspension was stirred at 45° C. for a period of two hours, while in the presence of chlorine (0.7 g), added to the slurry at the beginning of the contact.
  • the slurry was filtered, the cake rinsed with KCl brine (200 g KCl/L) and then washed with water.
  • the combined brine filtrate, rinsings and washings were analyzed for gold, silver and zinc.
  • the gold recovery was of the order of 87%; the silver recovery was of the order of 61%; and the zinc recovery was of the order of 99%.
  • Essentially all of the arsenic was found in the barren solid, and none was present in the brine or water rinsings.
  • Egleston In: The Metallurgy of Silver, Gold and Mercury in the United States, 1:261, John Wiley, 1887.

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US20090038951A1 (en) * 2007-08-10 2009-02-12 Rohm And Haas Electronic Materials Llc Copper plating bath formulation
US20120328494A1 (en) * 2011-05-02 2012-12-27 David Dreisinger Method for recovering indium, silver, gold and rare, precious and base metals from complex oxide and sulfide ores
EP2771491A4 (en) * 2011-09-27 2015-07-29 Dundee Sustainable Technologies Inc METHOD AND SYSTEM FOR GOLD EXTRACTION WITH HALOGENS
US9206492B2 (en) 2014-03-12 2015-12-08 Dundee Sustainable Technologies Inc. Closed loop method for gold and silver extraction by halogens
WO2016048750A1 (en) * 2014-09-24 2016-03-31 Ecolab Usa Inc. Method for recovering gold from refractory ore
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
CN110453075A (zh) * 2019-08-26 2019-11-15 华南理工大学 一种从废线路板金属富集体粉末中回收铜的方法
CN110551897A (zh) * 2019-08-26 2019-12-10 华南理工大学 一种机械物理法处理废线路板制备纯铜粉末的工艺
US10544480B2 (en) 2015-05-13 2020-01-28 K+S Chile S.A. Agglomeration drum for pre-treating minerals
CN115433825A (zh) * 2022-08-16 2022-12-06 湖南中邦再生资源科技有限公司 一种废旧锂电池中铁和硫的综合回收方法
WO2025043273A1 (en) * 2023-08-25 2025-03-06 Minetometal Pty Ltd Recovering metal values from complex concentrates

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AU2008300274B2 (en) * 2007-09-18 2012-04-19 Barrick Gold Corporation Process for mercury control during pressure oxidation
US9771631B2 (en) * 2009-05-26 2017-09-26 Metaleach Limited Method of oxidative leaching of sulfide ores and/or concentrates
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CA2821467C (en) 2013-07-18 2019-12-24 Nichromet Extraction Inc. Method for gold recovery on particules
WO2015135053A1 (en) * 2014-03-12 2015-09-17 Dundee Sustainable Technologies Inc. An improved closed loop method for gold and silver extraction by halogens
CN104694764B (zh) * 2015-03-09 2016-08-24 中南大学 一种细粒级包裹金的强化浸出方法
US10167202B2 (en) 2016-02-23 2019-01-01 King Abdullah University Of Science And Technology Enhanced metal recovery through oxidation in liquid and/or supercritical carbon dioxide
MX2018016084A (es) 2016-06-24 2020-02-05 Enviroleach Tech Inc Métodos, materiales y técnicas para recuperar metales preciosos.
US10526682B2 (en) 2017-07-17 2020-01-07 Enviroleach Technologies Inc. Methods, materials and techniques for precious metal recovery
CN109852795B (zh) * 2019-03-12 2021-07-30 大冶有色设计研究院有限公司 一种提高难选冶金矿石的选冶回收率的综合回收方法

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Cited By (15)

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Publication number Priority date Publication date Assignee Title
US20090038951A1 (en) * 2007-08-10 2009-02-12 Rohm And Haas Electronic Materials Llc Copper plating bath formulation
US7857961B2 (en) * 2007-08-10 2010-12-28 Rohm And Haas Electronic Materials Llc Copper plating bath formulation
EP2022875A3 (en) * 2007-08-10 2011-06-22 Rohm and Haas Electronic Materials LLC A Copper Plating Bath Formulation
US20120328494A1 (en) * 2011-05-02 2012-12-27 David Dreisinger Method for recovering indium, silver, gold and rare, precious and base metals from complex oxide and sulfide ores
US8585991B2 (en) * 2011-05-02 2013-11-19 South American Silver Corp. Method for recovering indium, silver, gold and rare, precious and base metals from complex oxide and sulfide ores
EP2771491A4 (en) * 2011-09-27 2015-07-29 Dundee Sustainable Technologies Inc METHOD AND SYSTEM FOR GOLD EXTRACTION WITH HALOGENS
US9206492B2 (en) 2014-03-12 2015-12-08 Dundee Sustainable Technologies Inc. Closed loop method for gold and silver extraction by halogens
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US7537741B2 (en) 2009-05-26
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MXPA03011413A (es) 2004-08-16

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